JP6554384B2 - Method and apparatus for treating carbon-containing feedstock into gasification gas - Google Patents

Description

  [0001] The present invention relates to solid state wastes and industrial wastes, fossil fuels, and other carbon-containing feedstocks gasified by using chemical techniques and equipment, in particular pyrolysis and downflow gasification processes. Method and apparatus for processing.

  [0002] This application claims the priority of US Provisional Patent Application 61 / 314,002, filed March 15, 2010, which is incorporated herein by reference in its entirety.

  Downflow gasification processes have a number of advantages over upflow gasification processes, which are processes commonly used in modern technology for processing carbon-containing feedstocks. . One such advantage of the downflow gasification process is that process tar, acid, and steam formed in the low temperature pyrolysis zone are passed through the combustion and reforming zone where they are exposed to the gasification gas under exposure to high temperatures. It is about to reach almost complete conversion. This allows such gases to be used to produce electrical energy in gas-diesel engines, gas powered engines, or gas turbines, for example, with minimal cost for cooling and purification of the gas.

  [0004] At the same time, the traditional downflow gasification process is characterized by several drawbacks, which have prevented the wider use of this process. Some disadvantages of the traditional downflow gasification process described in the technical scientific literature are: (1) the feed is packed tightly into the reservoir for drying and low temperature pyrolysis, which makes it unstable It is impossible to use a downflow process for a method of plasticizing and coking a feed with a high content of volatile components because a complete gasification process occurs followed by a complete shutdown. (2) it is impossible to operate with a feed having a fine or large fraction, a feed showing a cohesive compact, or a feed having a high ash content with a low ash melting temperature; 3) There is a need to stop the process for periodic loading or additional loading of feed material, its manual grinding and plugging (called "Poking") And (4) the need to periodically remove residual ash and / or slag residue; (5) the v and the composition of the product gas become uneven due to the termination for loading the feed material, and Makes it more difficult to use such gas; (6) low relative productivity of the gasifier caused by the supply of air flow with parameters that cannot initiate vigorous slag formation process; (7) The formation of toxic inorganic residues; (8) the heat of the product gas can not be used efficiently to improve the gasifier efficiency; and (9) large heat losses.

  [0005] The following is a summary of the representative aspects of the present invention. This is provided as an introduction to help those of ordinary skill in the art to more quickly understand the detailed discussion that follows, and how the appended claims are set forth to illustrate the invention. Nor is it intended to be limiting.

[0006] One aspect of the apparatus of the present invention includes an outer container and an inner container, the inner container being disposed within the outer container, thereby forming a gap between the inner and outer containers. The apparatus also includes an elongated loading mechanism trunk and a loading mechanism having a feed supply system for moving the feedstock along the elongated loading mechanism trunk. The apparatus further includes a gasifier trunk, a combustion chamber, a gas outlet, and a slag discharge mechanism.

  [0007] Operation of the apparatus described above continuously feeds the feed material into the gasifier trunk, where the feed material is fed under pressure generated by the loading mechanism, whereby the feed material is loaded by the loading mechanism Move along the trunk and gasifier trunk, allowing the gas and residual carbon that forms to pass unimpeded through all treatment areas, followed by cooling, mechanical crushing, and slag removal including.

  [0008] One aspect of the novel method of the present invention provides a loading mechanism trunk; provides a drying zone; provides a plasticizing zone; provides a pyrolysis zone; provides a combustion zone; provides a reforming zone; Feed zone; feed material; by a loading mechanism having an elongated loading mechanism trunk and a feeding material supply device, feed material through the loading mechanism trunk and in the drying zone, pyrolysis zone, combustion zone, reforming zone, and Sending through each of the slag discharge areas; Such a method forms a plug which, by feed material, substantially hermetically separates the drying zone, plasticizing zone, pyrolysis zone, combustion zone, reforming zone, and slag discharge zone from the atmosphere; and is fed within the drying zone Forming and separating water vapor from the material; causing pyrolysis gas to form in the pyrolysis zone; separating substantially all of the pyrolysis gas from the feedstock in the pyrolysis zone, thereby separating carbon char residue; And forming a gasification gas; further comprising a step.

FIG. 1 shows a schematic diagram of an apparatus according to an aspect of the present invention. [0010] FIG. 2 is a schematic view of the distribution of the active area in a device implementing one aspect of the method of the present invention. [0011] FIG. 3 is a flowchart of one aspect of the method of the present invention.

  [0012] The present invention relates to methods and apparatus for treating a carbon-containing feedstock to gasification gas. The following description is presented to enable one of ordinary skill in the art to make and use the invention and is provided in the context of this description and its requirements. Although the invention has been described in relation to methods and apparatus for treating household and industrial waste, various modifications to the preferred embodiments will be readily apparent to those skilled in the art and the principles described herein may be It can be applied to modifications of other carbon-containing feeds, some aspects of the apparatus, and methods.

  [0013] The present invention provides feeds having various morphological structures, segmented compositions, and increased moisture content that have not been able to be processed reliably and efficiently in downflow processes according to previously known methods. It is possible to process the material.

Referring to FIG. 1, one aspect of the apparatus of the present invention includes an outer vessel 1, an inner vessel 2, a combustion chamber 3, a loading mechanism trunk 35 , and a slag discharge mechanism 5.
[0015] The outer container 1 is preferably made of sheet heat resistant steel in the form of a cylinder, but may be made of other heat resistant materials and may have a non-cylindrical shape. A cooling flange 10 having an annular air cooling channel 11 is preferably attached to the lower end of the outer container 1. A flange 12 is attached to the upper end of the outer container 1. A gas outlet 13, preferably having a rectangular or circular cross section, is arranged tangential to the outer container 1. The gas outlet 13 is for discharging the generated gasification gas from the apparatus of the present invention.

[0016] Preferably, a thermal jacket 14 is disposed on the outer surface of the outer container 1. An air flow path 15 is formed in the thermal jacket 14. The thermal separation jacket 14 is preferably provided with an outer casing 16 and a mounting pad 17. In another aspect, the outer casing 16 can be formed as two cylindrical shells of different diameter attached together by a rigid concentric bridge and attached to the lower flange 10. A cover 18 is attached to the upper flange 12. A flange 19 is disposed on the lower portion of the cover 18. An air distribution box 20 is attached to the upper surface of the flange 19. The flange 19 is connected to the flange 12. The flange 19 is also connected to the upper part of the inner container 2.

  A main body 9 of the slag discharge mechanism 5 is attached to the lower flange 10. A flange 23 having an air cooling channel 24 is disposed above the slag discharge mechanism 5. An air channel 48 passes through the flanges 10 and 23 and connects the air cooling channels 11 and 24.

  [0018] In this embodiment, the inner container 2 is characterized by having a cylindrical shape, and is made of sheet-like heat-resistant steel. The inner container 2 is disposed inside the outer container 1. The inner container 1 and the outer container 2 are connected via a flange 19. A gas flow path 26 is disposed between the outer vessel 1 and the inner vessel 2.

  A cover 21 is connected to the upper part of the inner container 2 via a flange having an air dispersion shell 20. A combustion chamber 3 is arranged in the lower part of the inner vessel 2. A gasifier trunk 8 is disposed inside the inner vessel 2. An air supply flow path 25 disposed inside the inner container 2 connects the air dispersion shell 20 to the combustion chamber 3. The air supply flow path 25 can be formed using a pipe. The blades of the stirring device 27 are formed on the outer surface of the inner vessel 2.

  [0020] In a preferred embodiment, the combustion chamber 3 is formed of heat resistant steel. Alternatively, the combustion chamber 3 may have a welded construction or may be in any other suitable manner. The combustion chamber 3 is characterized by having an inner wall 28 and an outer wall 29. Further, in a preferred embodiment, the combustion chamber 3 is secured together by a concentric insert that forms an interior volume—a sub tuyal bend 30-connected to the air distribution shell 20 by an air supply channel 25. It consists of a cylindrical shell.

  [0021] The inner wall 28 of the combustion chamber 3 may have the shape of a truncated cone having a wider diameter at its bottom. A heat-resistant coating can be applied to the outer surface of the combustion chamber 3. The outer tuyere 31 can be configured as a nozzle around the periphery of the inner wall 28.

  [0022] The inner tuyere 32 is arranged at a central portion of the combustion chamber 3 with a predetermined angle with respect to the wall of the inner vessel 2. The internal tuyere 32 is connected to the air distribution shell 20 by an air supply channel 25.

  [0023] The loading mechanism 7 includes a receiving bunker 33, a feed material supply channel 34, and a loading mechanism trunk 35. The loading mechanism may be equipped with a piston 36 or other suitable mechanical drive of design. In a preferred embodiment, the gasifier trunk 8 is located inside the inner container 2, with the axis of the gasifier trunk 8 substantially coincident with the axis of the loading mechanism trunk 35, and the lower open end of the loading mechanism trunk 35. Arranged so that 4 is placed at or slightly below the level of the upper end of the gasifier trunk 8. The diameter of the loading mechanism trunk 35 is smaller than the diameter of the gasifier trunk 8.

[0024] In another aspect, a portion of the loading mechanism trunk 35 located on top of the cover 21 can be equipped with a cooler. The gasifier trunk 8 is formed as a truncated cone which widens towards the bottom. Preferably, a deaeration slit is formed in the wall of the gasifier trunk 8. The deaeration slit is preferably cut over the entire length of the wall of the gasifier trunk 8, but preferably an uncut portion may remain in the vicinity of the central portion of the gasifier trunk 8. In a preferred embodiment, the degassing slit is wider towards the lower end of the gasifier trunk 8. The diameter of the bottom portion of the gasifier trunk 8 is smaller than the diameter of the inner vessel 2.

  [0025] In a preferred embodiment, the gasifier trunk 8 is reinforced along its length by steel rings of various diameters attached to the outer surface of the gasifier trunk 8. Such a steel ring functions as a rigid structure. If the shape of the gasifier trunk is different, the rigid structure is matched to the shape of the gasifier trunk. For example, if the gasifier trunk is octagonal, the rigid structure is also octagonal. Furthermore, in a preferred embodiment, the gasifier trunk 8 is equipped with rigid ribs arranged on the wall portions separated by the deaeration slit.

A humidification chamber 37 is formed between the inner container 2 and the gasifier trunk 8.
The slag discharge mechanism 5 has a cylindrical main body 9. A flange 23 is attached to the upper part of the cylindrical main body 9. An air flow path 48 is provided in the flange 23. An air dispersion box 39 is attached to the inner surface of the bottom 40 of the slag discharge mechanism 5. The air distribution box 39 is preferably cylindrical with a hole in its upper part. A branch pipe of the air supply flow path 38 is inserted through the side wall of the slag discharge mechanism 5 and attached to the air dispersion box 39 in a tangential direction.

[0028] The slag discharge mechanism 5 is equipped with a table 41. A rotating slag scraper 42 is disposed on the table 41. The rotary slag scraper 42 is configured as a hollow structure having an air cooling or water cooling system inside. The slag scraper 42 is equipped with a coolant injection branch pipe 45 and a coolant discharge branch pipe 46. Further the slag scraper 42, the bearing unit及 beauty mechanical drive device 43 is also equipped. The table 41 is attached to the main body 9 of the slag discharge mechanism 5.

  [0029] The flange 23 is an extension of the table 41. An air flow passage 48 is disposed between the flanges 23 and 10, and the air cooling flow passage 11 is connected to the tray 24 of the slag discharge mechanism 5 by the air flow passage 48. One or more slag recovery bunkers 47 are attached to the lower surface of the table 41. The slag recovery bunker 47 is connected to the slag discharge lock channel 6.

Preferred mode of operation:
[0030] The feed is loaded into the receiving bunker of the loading mechanism 33. Next, a batch of feed material is introduced into the feed material feed channel 34. The feed material can be moved by a piston equipped with a drive. Thus, a batch of feed is preferably introduced into the inclined feed feed channel 34 and then into the loading mechanism trunk 35. Once the batch of feed material has been moved into the loading mechanism trunk 35, the piston 36 is placed in its upper position. After the batch of feed material has been introduced into the loading mechanism trunk 35, the piston 36 driven by its drive is lowered to its lower position so that the feed material moves down the loading mechanism trunk 35. Under pressure applied by the piston 36 and the frictional forces between the compressed feed material and the inner wall of the loading mechanism trunk 35 combine to form an airtight plug from the feed material.

[0031] Synchronize the drive and piston of the feed supply channel 34 with the operation of the loading mechanism trunk 35. This makes it possible to batch feed compressed feed material in the form of airtight movable stoppers into the gasifier trunk 8. During the next loading cycle, a new plug formed in the loading mechanism trunk 35 pushes the previous one down into the gasifier trunk 8. Since the diameter of the gasifier trunk 8 is larger than the diameter of the loading mechanism trunk 35, the feed in the form of a compressed gastight plug collapses into smaller parts and the entire surface of the upper part of the gasifier trunk 8 Scattered over.

  [0032] In the loading mechanism trunk 35, airtight plugs are not allowed to dry out or burn out during operation, particularly when the gasifier is shut down (which may result in loss of plug confidentiality). Can be equipped with an external cooler. The gasifier trunk 8 is configured as a frusto-conical that widens towards its bottom. The degassing slit, also widened towards the bottom, reduces the friction between the feed and the inner wall of the gasifier trunk 8 (as the feed moves down the gasifier trunk 8). And facilitates the feed material to move through the gasifier trunk 8 and into the combustion chamber 5.

  [0033] Feed material compressed along its entire length in the gasifier trunk 8 is produced in the area of the combustion chamber 3 and directed to the gas outlet 13 through the gap between the inner vessel 2 and the outer vessel 1. It is exposed to the external heat from the wall of the inner vessel 2 which is heated from the outside by the hot gas that is being The temperature along the gasifier trunk 8 reaches about 700 ° C. in its lower part and about 300-400 ° C. in its upper part.

  [0034] A stirrer 27 comprised of a plurality of metal blades mounted in a spiral pattern on the outer surface of the inner vessel 2 transfers heat from the upflow of the hot gasification gas to the wall of the inner vessel 2 Increase.

  [0035] The continuous movement of the piston 36 moves the feed material inside the gasifier trunk 8 downward toward the combustion chamber 3. As it moves down the gasifier trunk 8, the feed material undergoes changes caused by exposure to heat. The low temperature treatment of such feedstocks can be roughly divided into three stages: drying, plasticization, and low temperature pyrolysis. Thus, the gasifier trunk 8 represents an area-area 1 of low temperature treatment. FIG. 2 illustrates the various areas within the device according to the invention.

Zone 1 has roughly three areas:
-Area 1.1 feed drying zone;
-Region 1.2 plasticizing zone; and-Region 1.3 low temperature pyrolysis;
Can be divided into

[0036] The low temperature treatment of the feedstock in zone 1 forms process steam and a pyrolysis gas comprising light tar and carbon. Such steam and gas are introduced into the humidifying chamber 37 through the degassing slit of the gasifier trunk 8. The humidification chamber 37 is disposed between the gasifier trunk 8 and the inner container 2. The process steam and the pyrolysis gases are then introduced into the area of the combustion chamber 3 through the gap formed by the difference in diameter of the lower part of the gasifier trunk 8 and the inner vessel 2. Due to the air-tight plug formed from the feed material in the loading mechanism trunk 35, the water vapor-gas mixture formed in the area 1 is not released into the atmosphere. The same stopper prevents outside air from entering. The light tar and carbon block the lower part of the humidification chamber 37 together with the pyrolysis gas formed in the low temperature pyrolysis zone (region 1.3) and passing through the degassing slit of the gasifier trunk 8. there is a possibility. However, due to the high temperature of about 1300 ° F. (about 704.4 ° C.) and the water vapor introduced from the drying zone (region 1.1), the lower part of the humidification chamber 37 is detarred, thereby providing a humidification Unobstructed passage of the steam-gas mixture from the chamber 37 into the combustion chamber 3 is possible.

[0037] In the plasticization zone (region 1.2) there are no degassing slits. This is because the feed material whose assembly state has changed from solid to viscous under the pressure of the piston 36 is extruded in this region through the degassing slit into the humidifying chamber 37 (this is a steam-gas mixture). This is necessary to avoid the possibility of forming obstacles to free passage.

  [0038] An air supply passage 25 is disposed in the humidification chamber 37 on the opposite side of the degassing slit of the gasifier trunk 8. Air heated from the wall of the slag discharge mechanism 5 is supplied from the air dispersion shell 20 to the inner tuyere 32 through the air supply channel 25 and to the outer tuyere 31 through the tuyere lower bent portion 30. The

[0039] Steam and / or carbon dioxide may be introduced into the gasifier as a further oxidant through a steam inlet 49 disposed in the upper portion of the humidification chamber 37.
[0040] An internal tuyere 32 is disposed at the level of the lower end of the gasifier trunk 8. The inner tuyere 32 is installed at an angle of about 45 ° with respect to the wall of the inner container 2. A plate holder is attached to the inner tuyere which also supports the feed material in the gasifier trunk 8 to prevent the feed material from suddenly falling into the area of the combustion chamber 3. Also give. The plate holder also helps the feed material separate into pieces. This allows the air from the outer tuyere 31 to freely penetrate into the compressed feed together with the gas from the humidification chamber 37, so that the residual carbon gas in the area of the combustion chamber 3. Process is promoted.

[0041] After passing through the cold treatment zone (zone 1), the residual carbon, which is divided into steam-gas mixture and fragments and partially crushed, under the action of the piston 36, is subjected to high temperature treatment. It is introduced into the combustion chamber 3 in which the zone (zone 2) is located. Zone 2 is characterized by having a temperature in the range of about 1300 ° F. (about 704.4 ° C.) to about 2400 ° F. (about 1315.6 ° C.) , as shown in FIG. The gas mixture and residual carbon are subjected to high temperatures.

-Area 2.1 High temperature pyrolysis and subsequent gasification zone;
-Area 2.2 combustion zone;
-Area 2.3 reforming zone.

The combustion chamber 3 is arranged in the lower part of the inner vessel 2 and is composed of a hollow tuyere lower bent portion 30 having an outer wall 29 of the combustion chamber 3 and an inner wall 28 of the combustion chamber 3. An air supply flow path 25 is attached to the upper portion of the inner wall 28 . An outer tuyere 31 is disposed along the entire circumference of the central portion of the inner wall 28 .

  The internal tuyere 32 is disposed inside the combustion chamber 3. A tuyere bending portion is formed by the outer tuyere 31 and the inner tuyere 32. Residual carbon and water vapor-gas mixture move from the humid chamber 37 along the tuyere bend under the action of the piston 36. Air heated from the wall of the slag discharge mechanism 5 is introduced into the tuyere lower bent portion 30 through the air supply passage 25, and further heated while cooling the metal structure of the tuyere lower bent portion 30. .

[0044] The heated air is introduced into the combustion zone (region 2.2) of the combustion chamber 3 at a velocity of about 30 to 50 m / s through the external tuyeres 31. Heated air is also fed into the combustion zone through the inner tuyere 32 at approximately the same rate. Initially, under the influence of air oxygen in the combustion zone, substantially complete combustion of the high energy gas and tar formed in the low temperature process (zone 1) and partial combustion of residual carbon occur. Due to the large exothermic effect of the oxidation reaction in the combustion zone (region 2.2), the temperature rises rapidly to about 2700-3100 ° F. (about 1482.2-1704.4 ° C.) , thereby increasing the moisture content. It is possible to further increase the amount of gasification gas produced by the hydrogenated gasification product as well as using a feed material having a content.

[0045] Next, by increasing the moisture content of the feed, the temperature in this zone can be reduced to 1600-2400 ° F. (871.1-1315.6 ° C.) . Due to the high velocity of the air from the tuyere, the combustion of the residual carbon in the immediate front of the tuyere is greatly increased (up to 200%) compared to the total burn rate in the combustion chamber 3. This loosens the residual carbon mass present in the area of the tuyere bend and causes a strong carbon boiling effect in the gas formed as a result of gasification in the same area, causing the combustion reaction and primary in this area. It is possible to increase the effect of the reforming reaction and greatly improve the composition of the gasification gas generated thereby.

[0046] Residual carbon that was not gasified in the combustion zone (region 2.2) descends into the reforming zone (region 2.3), where it participates in the secondary reforming reaction and complete gasification occurs. Done. In this reforming zone (region 2.3), the low temperature treated gas and tar that did not react with the air oxygen in the combustion zone (region 2.2) will eventually be converted from hot residual carbon and slag. Reduced to a level of simple combustible gas under the influence of high temperature. The reforming reaction taking place in the reforming zone (region 2.3) has a very pronounced endothermic property. This reduces the temperature in this area and the temperature of the treated gasification gas to about 1300-1450F (about 704.4-787.8C) .

  [0047] The inorganic components of residual carbon in the combustion zone (region 2.2) and reforming zone (region 2.3) act as adsorbents, and contain heavy metals, sulfur and chlorine compounds from the resulting gasification gas. Actively involved in the removal of harmful contaminants, they are converted to an inert form insoluble in water, ie mainly to composite silicate slags.

  [0048] The degree of gas purification and slag formation temperature in these areas is directly dependent on the constituents of the inorganic components in the residual carbon. Thus, the degree of gas formation and temperature of slag formation can be adjusted using mineral additives in the feed such as metal oxides, salts and hydrates of these oxides, silicon dioxide etc.

  [0049] Slag formed in the combustion zones (region 2.2) passes through the reforming zone (region 2.3) into the slag zone (zone 3), the temperature in these zones, the feed structure and Depending on the moisture content and the further feed of the inorganic feed additive and possibly the process stream into the gasifier, it is transferred in the liquid, viscous or solid state. Within the slag zone (zone 3), the slag is cooled, mechanically crushed and then removed through the slag discharge lock channel 6.

  [0050] The flange 23 connects the slag discharge mechanism 5 to the gasifier vessel through the lower flange 10 of the outer vessel 1. A through-air channel 48 is disposed between the flanges 23 and 10, thereby connecting the air-cooled channel 11 and the tray 24 of the slag discharge mechanism 5. With the help of the cold air supplied to the gasifier by the system of the air flow path, the flanges 23 and 10, the body and other members of the slag discharge mechanism 5, and the lower part of the outer container 1 (all of which are hot The temperature acting on the area) is reduced.

  [0051] The air heated in the tray 24 of the slag discharge mechanism 5 is supplied to the air dispersion box 20 disposed on the cover 12 through the vertical air flow path 15, and then the air is supplied to the interior of the combustion chamber 3. And send to the outside tuyere. The body 9 of the slag discharge mechanism 5 is attached to the table 41 at its transition point to the flange 23. The body 9 has a bottom 40. An air distribution box 39 is arranged on the inner part of the bottom 40. The air distribution box 39 is preferably configured in the form of a cylinder with concentric holes in its cover.

The air supply flow passage 38 is introduced through the side wall of the main body 9 of the slag discharge mechanism 5. Low temperature ambient air is supplied into the gasifier through the air supply channel 38. The air supply flow path 38 is preferably connected to the air distribution box 39 at an angle that improves the air distribution inside the air distribution box 39. A rotating slug scraper 42 is disposed on the table 41. The slag scraper is cooled from the air distribution box 39 by the air flow. Slag scraper 42 may be equipped with its own air or water cooling system, coolant inlet 45, coolant outlet 46, bearing block 44, and mechanical drive 43.

  [0053] During rotational movement under the action of the mechanical drive 43, the slag scraper 42 scrapes off a portion of the upper solid slug with its toothed edges, while this also sharpens the front of it. At the edge, the slag is scraped off the surface of the table 41, which is introduced in molten form but subsequently solidifies on the surface of the table 41 as a result of cooling by the air supplied continuously into the tray 24. The slag is crushed and extruded under the action of the centrifugal torque of the slag scraper 42 around the periphery of the table 41 on which one or more slag accumulation bunkers 47 are arranged. The slag accumulation bunker is connected to the slag discharge lock channel 6. Thus, the slag accumulation bunker 47 is filled with the crushed slag. Thereafter, the upper slide gate (not shown in FIG. 1) of the locking device is opened and the slag is drained into the locking device, whereby the slag accumulation bunker 47 is emptied. The upper slide gate is then closed and the lower slide gate (not shown) is opened, thereby discharging the slag from the locking device. Next, the slag is sent into the slag accumulation bunker by the transfer device (not shown). This process makes it possible to discharge the slag substantially without the ambient air entering the gasifier.

  After passing through the high temperature treatment area, gasification gas is introduced into the gas area-area 4 which is arranged in the area between the outer vessel 1 and the inner vessel 2. The gas flow passes through the gap between the inner vessel 2 and the outer vessel 1 from the lower part of the combustion chamber 3 to the gas outlet 13 upwards from the bottom, while the gas flow passes through the inner vessel 2 in the zone of the cold treatment (zone 1). ) Is cooled to a temperature of about 300-400 ° C. for convective heat transfer. A stirrer 27 is installed in the gas zone (zone 4) to facilitate heat exchange.

  [0055] A gas flow rising upward from the bottom is introduced into the stirring device 27, where it moves in a helical trajectory around the inner vessel 2 and changes its direction of movement as it moves. This increases both the linear velocity and turbulence of the gas flow. These two factors, combined with the increased heat exchange surface (due to the surface of the blades of the stirrer 27), greatly improve the heat transfer rate between the gas and the inner vessel 2, thereby the low temperature treatment area (area 1 ) The maximum amount of heat is transferred from the gasification gas to the feed.

  [0056] In order to avoid further resistance to the gas flow leaving the stirring device 27, the gasification gas outlet 13 is preferably mounted tangentially on the outer vessel 1 with a downward slope. This, coupled with the high velocity of the gas flow through the gas outlet 13, minimizes the deposition of carbon and slag dust that may be present in the gasification gas on its lower wall.

  [0057] The gas outlet 13 has external insulation, and through a flange joint, a heat insulating casing (which can minimize heat loss of gasification gas through the walls of the cyclone separator vessel). It is connected with a high temperature cyclone separator. A hot cyclone separator is used to clean and remove finely dispersed carbon and slag dust from the gasification gas discharged from the gasifier, which is collected in a receiving bottle and removed through a locking device. Can do.

  [0058] The gasification gas can be further sent to a system for cooling and final purification, where cooling can be performed to produce a process stream or hot water, while its further industrial application Final removal of harmful contaminants may be necessary.

[0059] For a better understanding of the present invention, but without limiting its scope, a description of the temperature zone is given below.
Temperature range:
[0060] In the apparatus of the present invention, the heating, drying, low temperature and high temperature pyrolysis processes of the feed are performed simultaneously. Furthermore, the interaction of the oxidizing gas with the decomposition products and the residual carbon of the feed occurs in the apparatus.

  [0061] Solid household waste (SHW) as a feed for gasifier devices is a highly diverse and multi-component composition of organic and inorganic components. Table 1 includes data on which the following discussion is based.

  [0062] The organic and inorganic components of the feed are essential for the processing of the feed. These greatly affect both the composition of the gasification gas produced and the formation of residual slag. Both the composition and the type of inorganic component influence the processing of the feed. Two major types of inorganic components are distinguished as mechanical contaminants and components that are chemically bonded to the feed contents.

[0063] The first major type comprises the inorganic component in an amount ranging from about 6% to about 25% of the total weight of the feed. Components of this type are found in feed materials as mechanical contaminants such as non-ferrous and ferrous metals, ceramics, construction waste, rubbish, glass etc. and form the inorganic part thereof, CaCO ₃ , MgCO ₃ , FeCO ₃ , CaSO ₄ , Na ₂ SO ₄ , FeSO ₄ , FeS ₂ , SiO ₂ , silicate with various contents of main oxides: Al ₂ O ₃ , SiO ₂ , CaO, Na ₂ O , K ₂ O, and small contents of other metal oxides.

[0064] These components can be arranged symbolically, reducing their content in the feed in the following order.
-SiO ₂ - several tens of percent;
_{-Al, Al 2 O 3, MgO} , Fe, F 2 O 3, CaSiO 3, CaCO 3 - a few percent, several tens of percent;
_{-Cu, Zn, S, TiO 2} , FeO, Ni, Pb, Na 2 SiO 3, Sn, CaSO 4, MgSO 4, Cl -, S 2-, Na 2 CO 3 - a few percent, several tenths of a percent ;
_{-BaO, ZnO, Cd, NaCl,} NaPO 4, MgCO 3, MgSO 4, MgSiO 3, K 3 PO 4, CaCl 2, MgCl 2, K 2 CO 3, Cr, Sb, SbO- few tenths and a few One hundred percent;
_{-NaOH, LiOH, W, V 2} O 5, Cr 2 O 3, Ni 2 O 3, PbO, ZnSiO 3, F -, SO 3 2-, Mn, V, Mo, As, Co, Hg, As 2 O ₃ , BeO—less than one hundredth of a percent.

  [0065] The second type of inorganic component comprises a component that is chemically bonded to the feedstock and constitutes a smaller amount of the compound. This type of inorganic component usually constitutes 0.47% to 2.81% of the total weight of the feed. Some of these components are, for example, metals contained in paper, cardboard, wood and their oxides and salts, and dyes contained in fiber waste and polymeric materials.

[0066] low-temperature treatment zone having a temperature in the range of area 1 20 ~ 700 ℃. This area provides for the drying, destruction, and low temperature pyrolysis of the feedstock introduced into the gasifier. This area can be roughly divided into three regions according to the temperature range.

Area 1.1 Dry area. Temperature range is 20 ~ 0.99 ° C..
Area 1.2 Plasticized area. Temperature range is 0.99 ~ 350 ° C..
Area 1.3 Low temperature pyrolysis area. Temperature range is 350 ~ 700 ° C..

[0067] Zone 1. A drying area having a temperature in the range of 20O <0> C to 150 <0> C and disposed within the lower portion of the loading channel. Here, the following process is performed.
-In the cooling part of the loading mechanism trunk: compresses the charged feed material and forms an airtight plug. This is a process that substantially hardens the feed.

-In the area heated by the heat of the gasification gas in the upper part of the gasifier trunk: the feed material is first heated to evaporate free moisture.
-Vigorous water vapor formation; feed material drying (in which partial superheating of the water vapor takes place); initiates a process that changes the aggregate state of the fusible components of the feed material and softens the local areas in the feed material mass .

  [0068] In the context of the drying process, free moisture, moisture mixing with the fuel (ie moisture obtained in direct contact with water), and in the structure of the feedstock caused by water vapor adsorption The contained moisture (moisture absorption) is distinguished.

  [0069] During the heating process, the drying rate rises rapidly to a constant value, then a period of constant drying rate begins, and after reaching the hygroscopic state, the phase of decreasing the drying rate begins. The evaporation zone goes deep into the compressed feed mass. Evaporation of moisture from the surface and its transfer into the mass under exposure to hydrothermal conduction results in intense heating of the surface bed and moisture enrichment of the internal bed.

  [0070] During the drying process, the heat transfer coefficient decreases constantly. Starting from the critical point, the heat transfer coefficient also decreases dramatically with a decrease in moisture content caused by a deeper evaporation zone and increased thermal resistance of the dry outer bed of the feed.

  [0071] These processes lead to a deterioration in the warming of the inner bed of the feed, thereby increasing the time to completely dry the inner bed of the feed. Thus, the lower end of the dry area of the total feed in the gasifier trunk takes on a shape somewhat similar to a truncated cone with its apex at the bottom as shown in FIG.

  [0072] The water vapor formed as a result of the drying of the feed is introduced into the humidification chamber through a degassing slit in the gasifier trunk where it contacts the wall of the gasifier inner vessel and partially overheats. Will be

[0073] During the entire drying process, the feed material shrinks; in other words, the volume decreases, leading to larger structural changes by further warming it.
[0074] plasticizing zone having a temperature change in the range of the region 1.2 300 ~ 675 ° F (148.9~357.2 ℃) is arranged in the region which is heated in the center of the gasifier trunk In which the following process takes place.

-Complete drying of the feed material;
-Initiation of decomposition and destruction processes of organic polymers;
-Changing the aggregated state of fusible materials of organic and inorganic origin into a plastic or liquid state;
Conversion of the entire feedstock into a plastic transferable material; and initial formation of tar and saturated and unsaturated hydrocarbons.

  [0075] Thus, the polyethylene begins to melt at a temperature of about 120 ° C. As the temperature is increased, other polymers that exhibit a fusible portion of the feed begin to melt. When the temperature reaches about 200-250 ° C., all the polymer turns into a liquid material, filling all the voids in the feed mass. At the same time, the entire feed material is transformed into a plastic, gas-tight substance and slowly travels down the interior space of the gasifier trunk under the pressure exerted by the piston of the loading mechanism.

[0076] At a temperature of about 390 ° F. (about 198.9 ° C.) , the inorganic colloid converts to the water vapor phase. The resulting water vapor passes through the viscous mass of the feed material and proceeds into the drying zone, which is then introduced into the humidification chamber along with the water vapor formed in the drying zone.

  [0077] In the structural change process that takes place in the drying area, the entire feed material shrinks significantly, increasing its thermal conductivity, thereby promoting faster warming of the entire feed mass, including its internal parts. Is done. However, the inner part of the feed is still warmed more slowly than the outer part. Thus, the lower boundary of the plasticizing zone and its upper boundary take the form of an irregular cone having a vertex at the bottom as shown in FIG.

[0078] At a temperature of about 480 ° F. (about 248.9 ° C.) , gases such as carbon monoxide and carbon dioxide, and tar begin to evolve from the feed bed. As heating proceeds, methane, heavy hydrocarbon gas, and hydrogen begin to evolve. Such gas passes through the viscous mass of the feed and proceeds into the zone of low temperature pyrolysis. Such gas then flows into the humidification chamber through the degassing slit of the gasifier trunk.

  [0079] There are no degassing slits in the region of the gasifier trunk where the plasticizing zone is located during operation of the gasifier. This is done to avoid the feed material being squeezed into the dampening chamber. However, the water vapor formed in the upper part of the plasticization zone is introduced into the humidification chamber through the degassing slit of the drying area, while the tars and gases from the lower part of the plasticization zone are in the low temperature pyrolysis zone. It is introduced into the humidification chamber through the deaeration slit.

  [0080] Region 1.3 A low temperature pyrolysis zone having a temperature in the range of about 350 ° C to about 700 ° C is located in the lower warming portion of the gasifier trunk. The following process is performed in area 1.3.

-Changing the aggregated state of the refractory materials and transferring them to the plastic state;
Decompose and break down organic compounds to break up the covalent bonds in the polymer and the lattice of the organic compounds;
-Intense gas release;
Release light tar-like substances, solidify the plastic material and carbonize it, starting from the outer layer;
-Transfer the entire feed mass to residual carbon; and-decompose certain organic salts.

  [0081] The initial decomposition temperature of the feedstock is determined primarily by the individual properties of the feedstock, which is somewhat determined by the heating conditions. The higher the content of bound oxygen contained in the feed, the lower its initial decomposition temperature.

[0082] In the initial heating stage of the feed, the oxygen-containing component is then discharged first, and finally the tar-like substance with the least degree of oxidation is discharged. During heating, a large amount of oxygen in the feed is available, leading to an exothermic effect due to the oxidation reaction that is generated. This leads to further heating of the feed material, which accelerates its destruction. Such a process is further aided by the decomposition of some inorganic salts, thereby forming the corresponding oxides, in some cases oxygen and other salts, by warming the charged feed.

  [0083] The oxidation reaction promotes an increase in the temperature of the feed in this area, which depends mainly on water vapor, carbon dioxide, carbon oxide, acetic acid, methyl alcohol, formaldehyde, tar, depending on the morphology of the feed , Various decomposition products such as methane, ethane, propylene, and hydrogen, and also some other decomposition products are discharged.

  [0084] The availability of polymeric materials in the feed material will correspondingly increase the yields of ethylene and polypropylene. At the same time, the polymer decomposes substantially completely without forming residual carbon.

  [0085] The above described process of decomposing the feedstock and forming a gas greatly reduces the amount of feedstock and transforms its structure into a dense porous carbon form. Continuing the heating process substantially completes the discharge of tar-like material and other products that can be condensed upon cooling. Gas formation continues, but this continues with less intensity. Feed decomposition products formed as a result of low temperature pyrolysis are introduced into the humidification chamber through the degassing slit of the gasifier trunk. In the humidification chamber, such products are mixed with the water vapor from the drying zone and subjected to further warming under the action of thermal radiation from the wall of the internal vessel of the gasifier or from direct contact therewith. Tar and residual carbon particles that accumulate on the walls of the humidification chamber are removed by the high external temperature and water vapor from the upper drying zone.

  [0086] The inflow of the liquid fraction into the center of the trunk and the conical shape of the lower boundary of the area located on the solid carbon residue causes the plastic material of the feedstock to be extruded or the liquid fraction to be degassed in the trunk The possibility of flowing into the humidification chamber through is reduced.

  [0087] Zone 2-high temperature treatment zone; high temperature pyrolysis of the feed material having a temperature in the range of about 700 ° C to about 1300 ° C, and its gasification gas under exposure to air oxygen and other oxidizing agents It is characterized by performing further gasification.

[0088] This area is roughly divided into three regions according to the temperature range.
Region 2.1 High temperature pyrolysis zone. The approximate temperature range is 700-900 ° C.
Zone 2.2 Combustion zone. The approximate temperature range is 900-1300 ° C.

-Area 2.3 reforming zone. The approximate temperature range is 800-1100 ° C.
[0089] Region 2.1 A high temperature pyrolysis zone having a temperature in the range of about 700 ° C to about 900 ° C. The following process takes place in this area.

Final gas generation process;
-Changing the residual feed into a solid porous carbon mass;
-Decompose and melt the inorganic salt and interact it with the carbon and inorganic components of the feed.

[0090] Destruction of the fuel organics occurs with the formation of small amounts of methane, hydrogen, and trace amounts of other hydrocarbon gases.
[0091] A temperature of 900-1100 ° C is the highest temperature, at which the generation of volatile materials from solid residual carbon is complete.

[0092] In this zone, some carbonates: Na ₂ CO ₃ 851 ° C .; K ₂ CO ₃ 891 ° C .; Li ₂ CO ₃ 618 ° C. melt and interact chemically with the carbon and inorganic components of the feed. To do.

[0093] Especially, the concentrations of CO and CO ₂ produced in the gas increases. In addition, some chlorides melt. For example, CaCl ₂ 787 ° C .; NaCl 801 ° C. Molten chlorides and carbonates can form eutectic mixtures with more refractory salts, thereby lowering the latter melting temperature. This phenomenon has a significant effect on the formation of liquid slag having a subsequently reduced melting temperature.

[0094] Region 2.2 A combustion zone having a temperature in the range of about 900 ° C to about 1300 ° C. The following process takes place in this area.
-Combustion and thermal destruction of pyrolysis gas with low temperature treatment of the feedstock;
Combustion of some of the residual carbon in the feed;
Gas dynamic treatment: grinding of residual carbon mass by conversion of residual carbon to "boiling" bed state;
-Separation of residual carbon;
-Reforming of combustion gas by oxidation of residual carbon;
-Oxidation treatment and reforming reaction of residual carbon components; and-initiation of residual slag formation process.

  [0095] The combustion zone is the primary gasification zone, where it is split into fragments under the action of decomposition and oxidation of gaseous pyrolysis products and a dividing plate located in the lower part of the gasifier trunk and An intense interaction between the partially crushed residual carbon and air oxygen and other oxidizing gases takes place. Initially, only gaseous products are oxidized by air oxygen and, to a lesser extent, interactions with carbon dioxide and water vapor that are generated during the low temperature processing of the feed or supplied to the gasifier Done.

[0096] The limiting factors of the gas combustion process at a particular temperature are the diffusion rate and, for residual carbon, the surface area of the heterogeneous phase, the rate of oxygen adsorption, and the rate of reaction product desorption.
[0097] The combustion zone is symbolized as region 2.2 in the gasification zone, the lower portion of which comprises the reforming zone-region 2.3. The gas formation processes in these areas are just as complex and interrelated as the liquid slag formation process, so it is necessary to consider them together.

  [0098] Gasification can be described by simple chemical reactions (1)-(11) that reflect complex processes occurring within the combustion zone.

  [0099] The combustion process takes place in the upper portion of the combustion chamber under exposure to air oxygen supplied through external and internal tuyere forming tuyere plates in which the combustion zone is located.

[00100] To increase the gasification process, air is warmed as a result of cooling of the gasifier components. Furthermore, steam and / or carbon dioxide can be injected into the combustion zone at a high rate. The air injected through the tuyere at high speeds (up to 50 m / sec) through the tuyere increases the residual carbon combustion process of the feed. Thereby, the temperature at the initial stage of jet combustion in the portion of the combustion chamber disposed in the area of the air tuyere, depending on the amount of steam and carbon dioxide, high exothermic reaction effects (1) to (3), The high calorific gas and tar burnout (6), (7), (8) formed in the low temperature processing zone of the feed and in the zone of high temperature pyrolysis can be raised to about 1500 ° C.

[00101] Air oxygen is substantially completely consumed in the oxidation reaction of pyrolysis gas with residual carbon, mainly carbon dioxide and water vapor are formed, the latter playing a major role in the gasification process. An oxidizing gas is also formed. Interacting with the residual carbon, these gases are reduced to predominantly simple combustible gases by reactions (9) to (11).

[00102] Increasing the hydrogenation gasification reaction (9), (10) for further warming of residual carbon and water vapor (both produced as a result of the oxidation process) by increasing the temperature in the combustion zone Can do. The elevated temperature in the combustion zone causes an increase in the hydrogenation gasification kinetics (9), (10), which can be used without first having to pre-dry the feed with an increased moisture content, Alternatively, it is possible to further supply water vapor from the outside.

[00103] Similarly, exposure to an initial high temperature causes a carbon dioxide gasification reaction of residual carbon in the jet (11), thereby using carbon dioxide supplied from the outside as a further oxidizing agent. It becomes possible.

[00104] Reactions (9), (10), (11) take place primarily in the second stage of the jet combustion process in the combustion zone. These are primary endothermic reforming reactions. Due to these reactions, the overall temperature in the lower part of the combustion zone drops to 900-1100 <0> C. Next, the action of the secondary reforming reactions (9), (10), (11) begins in the reforming zone of the gasifier and unreacted in the combustion zone under exposure to residual carbon dioxide and steam. As a result, gasification of residual carbon is led to change to combustible gasification gas.

[00105] The high velocity, up to 50,000 kg / m ² · h, of hot air injected through multiple tuyeres results in gasification of the feedstock within the area of the combustion chamber located directly in front of the tuyeres Increase. This, coupled with an increased amount of heated air introduced into the combustion zone,
Cutting, shattering and loosening the residual carbon and sending it from the gasifier trunk as a large sintered porous piece to the combustion zone;
-The strong boiling effect of residual carbon in the gas as a result of gasification improves the dynamic properties of the gas in the combustion zone, thereby making it possible to avoid the formation of local stagnant regions in this zone about;
Separating the pieces of residual carbon and lowering the larger and heavier part of the residual carbon ground mass into the gasification zone and gasifying the smaller part in the combustion zone;
-Temperatures not only in the area where the tuyere is arranged, but also throughout the combustion zone, thereby maximizing the gasification process and converting tar, acid and complex hydrocarbons in this zone Making it possible to increase the degree of
Double or triple the total strength of the gasification of the feed material, for example to increase the throughput across the entire cross section of the combustion chamber by 500 to 1500 kg / m ² · h; simple combustion like CO and H ₂ Producing gases with improved composition by their saturation with sex gases, thereby leading to high levels of hydrogenation gasification reactions (9), (10), and gasification of passing carbon dioxide (11); Then - as a result of the gasification air, ballast content in the total volume of the product gas (ballast _{CO 2, H 2 O, O} 2, and is of the form N ₂₎ reduces, gasification to produce by it Allowing the gas to be used more efficiently for electricity generation and other purposes;
Becomes possible.

[00106] The inorganic portion of the residual carbon also undergoes fundamental changes both chemically and structurally in the gasification zone.
[00107] Because of the high temperature, the salt decomposition process of the inorganic portion of residual carbon initiated in the low temperature pyrolysis zone is greatly increased in the combustion zone. Due to the effect of the supplied oxygen, complete or partial oxidation of some metals is possible in the part of the combustion chamber located in front of the tuyere.

[00108] In the same area, nitrogen: N and sulfur: S oxide: is oxidized to SO ₂ and NO _x. These amounts are determined by the starting content of such elements in the charged feed and the amount of free air oxygen in the combustion chamber.

[00109] In the combustion zone, formation reactions of NH ₃ , H ₂ S, and HCl, and other gases, which are harmful gaseous components that are subject to removal from the produced gas, occur.
[00110] Next, in the second stage of combustion, if oxygen is completely consumed for oxidation during the process of the primary reforming reaction, a portion of the oxide is subjected to the action of burning hot carbon. Reduced to metal and non-metal.

[00111] Especially, SO ₂ and NO _x are reduced to simple elements -S and N _2, which is further bonded to an oxide and a metal, the corresponding sulfides and nitrides are formed.
[00112] In addition, hydrogen sulfide -H ₂ S is formed happening reaction of sulfur dioxide -SO _2,
The latter forms the corresponding sulfide by interaction with the metal oxide.

  [00113] Similarly, halogens combine to form chlorides and fluorides of various metals.

[00114] NH ₃ may also react with some oxides and pure metals to oxidize to nitrogen or form nitrides.

[00115] In the presence of some unreacted water vapor in the gasification zone, a downflow process, ie hydrolysis of the salt, is also possible, but this is the activation of the hydrogasification process and within this zone This is minimal due to the presence of a large amount of free moisture.

[00116] The entire process continues in the reforming zone within region 2.3.
[00117] Region 2.3 A reforming zone having a temperature in the range of about 800 ° C to about 1100 ° C. This area is
-The process of the secondary reforming reaction;
-Removal of harmful components from the gas produced;
-Completion of the liquid slag formation process;
A final formation process of the gasified gas composition produced;
Is performed.

[00118] As a result of the processes carried out in the combustion and reforming zone, oxides of various metals, including carbon contaminants, and small amounts of undegraded salts and reduced pure metals of the inorganic portion of the feed It is formed. Depending on the starting composition of the feed, some amounts of metal alloys based on iron, copper and silicon may be formed.

[00119] Exposure to elevated temperatures can cause metal parts of oxides and pure metals and their salts to change to a gaseous state. However, most volatile metals and their compounds maintain a solid or liquid state. This can be explained by either the insufficient time they exist in the hot zone or the formation of other less volatile compounds such as some sulfides, silicates and chlorides. it can.

[00120] Sulfides, silicates, and various chlorides formed as a result of such reactions are
Actively involved in the formation of liquid residual slag.
The basic materials for forming the 00121] silicate slag, silicon dioxide: a SiO _2. If it is missing in the inorganic component of the feed, it must be added during the preparation of the feed.

[00122] While passing through the bed of slag formed, the gases produced in the combustion and reforming zone consist of harmful gas components, inorganic dust discharged with it, solid metal particles, and part of gaseous metals. Is then partially removed. Thus, the gas is introduced into the combustion chamber along with a small amount of mechanical contaminants such as inorganic dust, various heavy metals, and other harmful components.

[00123] Furthermore, due to the endothermic effect of the reforming reaction, the gasification gas at the outlet of the combustion chamber has a temperature in the range of approximately 700-800 ° C.
[00124] Table 1 shows possible distribution ratios of heavy metals in the slag, in the dust carried into the product gas, and in the product gas at the completion of the gasifier process.

[00125] However, the ratios given in Table 1 are the level of metal activity, their concentration in residual carbon, and inorganic in the feed, for example in the form of limestone, dolomite, and / or low purity iron ore. Determined by the presence of additives.

[00126] Typically, solid household waste contains a substantial amount of inorganic components. These concentrations increase as feedstock is introduced into the combustion zone. This is explained by a gradual decrease in the volume of the feedstock by removing moisture, gaseous products, and tars from it in the cryogenic treatment zone. Thus, the amount of inorganic additive can be reduced or not necessary at all.

[00127] It is important that the feed material includes a flux additive for liquid slag. The generated slag must be sufficiently movable and fusible to ensure uninterrupted operation of the gasifier. It is necessary that the slag formed be able to flow down the channels formed in the residual carbon mass downwards into the slag zone, where it is cooled by subsequent mechanical grinding and removal. Excessively thick and / or viscous slag can make the combustion and gasification zone less penetrating and, as a result, delay or completely stop the gasification process. Also, its removal from the gasifier can be substantially complicated.

[00128] Special additives such as flux can be used to facilitate slag passage and removal. If solid household waste is used as the feed, these additives may be minimal or not needed at all. This involves the process of residual slag formation, where the inorganic components of the feed are both chemically combined with the organic components (second group) and as mechanical contaminants (first group). Because.

[00129] The first group of small mechanical inclusions that are uniformly distributed in the organic portion of the feed after the pyrolysis zone is slightly protected from exposure to high temperatures by carbon, thus These are the main sources of slag formation.

[00130] The first group of large mechanical inorganic inclusions after the pyrolysis zone are also slightly shielded by carbon from exposure to high temperatures. However, nevertheless, due to their large size and weight, they pass quickly through the combustion zone and are introduced into the lower part of the reforming zone. They are joined by the more fusible fine mechanical inclusions or melt slowly to capture ash and slag particles.

[00131] In the pyrolysis process, after removing volatile components, a second group of inorganic compounds remain in the structure of residual carbon, which shields the inorganic components and heats them and further melts them. These melting at high temperatures only occur after carbon removal. These inorganic inclusions usually remain in solid form, not because of the basic slag formation process.

[00132] The formation of eutectics and heat resistant components with low melting points due to the increase in temperature in the combustion and reforming zone and the availability of large amounts of inorganic low melting point components formed as a result of the reforming reaction be able to. The resulting slag is free-flowing ash-like material with solid content of carbon, heat-resistant alloy, and inorganic particles that did not change to liquid state and large particles and did not melt or react chemically It is.

[00133] Solid slag in the reforming zone (its formation may be related to excessive moisture content in the feed, large amounts of refractory inorganic components in the feed, or insufficient addition of flux) If there is a buildup, this area may be completely or partially blocked with solid slag.

[00134] When this occurs, the residual carbon supplied from the gasifier trunk into the combustion chamber under the action of the loading mechanism exerts pressure on the slag mass. Thereby, slag is extruded from the combustion chamber section into the space of the slag section where the slag is cooled, crushed and removed from the gasifier.

[00135] Zone 3 Within this zone, the temperature is in the range of about 300 ° C to about 800 ° C, and the following process is performed.
-Cooling of slag;
-Mechanical grinding of slag;
-Take out the slag.

[00136] Slag is formed as a result of the processing of the feed in the combustion and reforming zone. The main components of the slag are metals and nonmetal oxides: SiO ₂ , Al ₂ O ₃ , Fe ₂ O ₃ , FeO, CaO, MgO, Na ₂ O, K ₂ O, and sulfides, chlorides, fluorides, It is a metal alloy and a content of unreacted carbon. Thus, slag is a complex amorphous and crystalline form of variable structure silicate with a small amount of mechanical contaminants.

[00137] The slag is introduced into the slag discharge area as a liquid, in the form of individual solid matter, or more rarely in the form of a lump of slag. Here, it is cooled slowly under the indirect action of cold ambient air introduced into the gasifier. As the slag reaches the metal plate table, it is cooled from the bottom by the air flow. The liquid fraction of slag solidifies quickly and is then cut by a rotating slag scraper.

[00138] A portion of the solid slag is cut by a notched edge at the top of the slag scraper, rotated by a mechanical drive. The slag is broken up and broken and removed from the peripheral area of the table where one or several locking channels are arranged. Next, the slag is taken out to the transfer device through the slag flow path for discharging from the gasifier. The locking passage allows the slag to be expelled while effectively preventing ambient air from entering the gasifier.

[00139] Zone 4 A gas zone having a temperature in the range of about 300 ° C to about 800 ° C. In this zone, it cooled to 300 ~ 400 ° C. The gas from 700 ~ 800 ° C..
[00140] After the reforming zone, the generated gasification gas is introduced into the gas zone located in the space between the outer vessel and the inner vessel of the gasifier. From the bottom, and passes upward through through the space between the outer container and the inner container of the gasifier, the gas stream is cooled to about 300 ~ 400 ° C. for release of heat in the area of low-temperature treatment . During this phase, gas “tempering” (which in the context of the present application means the final treatment of the gas composition) takes place.

[00141] A stirrer is installed in the gas zone to accelerate heat exchange. The agitation device is a multi-channel tunnel device that positions a spiral channel. A gas stream passing upwards from the bottom is introduced into the tunnel device, where it changes direction while moving in a spiral trajectory around the inner vessel of the gasifier. The gas flow increases at a linear rate and becomes turbulent, which improves heat exchange and allows maximum heat transfer from the gasification gas to the feed in the cryogenic treatment zone. Although tar is contained in the gas in an amount of 0.3 to 0.5 g / nm ³ , since the setting temperature of tar is less than 300 ° C., tar does not deposit on the wall of the stirrer or on the blade.

[00142] Next, the gas stream is sent into the hot cyclone separator through the gas outlet, where usually clean fine carbon and Suragudasuto contained in an amount of about ³ ~ 10g / nm 3 in the gas Removed. The fine carbon and slag dust thus removed is then removed from the device through the receiving bunker lock and sent to the transfer device for discharge from the gasifier.

[00143] The gasified gas is then sent to a cooling and final purification system where the cooling and removal of residual residues of harmful inclusions (this is suitable for power generation or other purposes) Is usually necessary) to be done.

[00144] Unless defined otherwise, technical and scientific terms used herein have meanings that are readily understood by those skilled in the art.
[00145] While not limited to the above description and possible modifications apparent to those of skill in the art, the following are some advantages that may be associated with the methods and apparatus described herein.

[00146] The high-speed hot air introduced through the external and internal tuyere systems, and the increased gas-forming reaction caused thereby, will reduce the throughput across the entire area of the combustion chamber to about 1,000-1500 kg. / M ² · hour can be increased. The actual throughput will depend on, among other factors, the feed morphological structure and moisture content.

[00147] The gasification gas produced has a relatively low temperature (in the range of approximately 300-400 ° C), is substantially free of acid, and the amount of tar is 0.3-0.5 g / nm ³ . The amount of finely dispersed carbon and slag dust is in the range of ^{3 to} 10 g / nm ³ .

[00148] The heavy metal is converted to an inert and insoluble silicate form with other harmful components and then removed from the gasifier along with the slag so that heavy metal oxides in the product gas The content is relatively low.

_[00149] The content of harmful gas components such as _{NO 2, NH 3, SO 2} , H 2 S, and HCl is minimal. At the same time, complex saturated and unsaturated gaseous hydrocarbons such as dioxins and furans are substantially absent in the product gas.

[00150] cooling and the after cleaning, resulting gasified gas is mainly CO, H _2, CH
₄ , composed of CO ₂ and N ₂ , the proportion of CO ₂ is substantially reduced to 0, and the content of N ₂ is such gas in standard gas-diesel, gas powered and gas turbine power generators Minimized to the level used in industry, its efficiency factor is twice as high as that of the steam units used in modern pyrolysis and gasification technology based on the upflow gasification process.

[00151] While not limiting the universality of the present invention, the following benefits can be obtained by implementing the apparatus according to the present invention.
-Solid household and industrial wastes, as well as other types of carbon-containing feedstocks can be used;
Reducing the requirements for the preparation of the feedstock and its costs;
There is no need to perform predrying of the feed material;
The entire feedstock treatment (pyrolysis and gasification) can be carried out in the same apparatus;
-Feed changes and slag discharge are performed automatically;
Oxygen-steam mixtures can be fed into the device together with hot air or air-steam mixtures, for which it is possible to produce gases of different quality for different applications ;
Due to the low levels of contaminants found in the product gas, simple techniques are used in cooling and purification / cleaning systems, which lowers the operating costs and revises the price of the equipment.

[00152] The following examples are given solely to illustrate the present invention and should not be construed as limiting its scope.
Example 1: Technical scheme of an apparatus for bed gasification under pressure:
[00153] Prepare feed material (eg, solid household waste) prior to introduction into the gasifier,
Excess inorganic components, particularly large fractions, are extracted from the feed and then the feed is crushed and broken. Depending on the morphological structure of the feed, special products such as limestone, dolomite, low-purity iron ore, and final chemical purification products of gasification gases such as Na ₂ S, NaCl, NaOH, FeO, Fe ₂ O ₃ etc. Additives can be added using a batch feeder. The feed material is then sent on the transfer device into the bunker of the loading mechanism and transferred into the processing device.

[00154] generated as a result of the processing of the feed material, the gasification gas having a temperature in the range of about 300 ~ 400 ° C. at the outlet from the device, through an outlet which is insulated, high temperature thermal isolation casing is attached Sent to the cyclone separator. Within this separator, the gasification gas is then cleaned beforehand of mechanical contaminants such as slag and some carbon dust.

[00155] Slag formed in the gasifier as a result of processing of the feed and having a temperature of about 200 ° C is fed through a lock channel to a transfer discharge device and sent into a storage bunker where it is further cooled Is done. The slag dust from the high temperature separator is withdrawn to the transfer and discharge device through the storage bunker and lock discharge channel where it is mixed with the slag from the gasifier and further transferred into the storage bunker.

[00156] After pre-removal of mechanical contaminants in the separator, the gasification gas is sent to a first heat exchanger and cooled by cold water, where the gas is cooled to about 40 ° C. At the same time, the cold water passing through the water treatment system is sent is heated to a temperature of about 60 ~ 80 ° C. in a second heat exchanger.

[00157] The first heat exchanger is fitted with a condensate receiver, where water condensed steam, residual tar not reacted in the gasifier, finely dispersed slag and carbon dust Is accumulated with the gas component of All condensed liquid, viscous and solid components are sent along with the condensed water from the condensate receiver through the batch feeder into the feed, which is fed into the gasifier or filter , Where excess water is removed and sent to the water purification system. The partially dehydrated residue is sent into the feed.

[00158] After the first heat exchanger, the partially purified gasified gas cooled to a temperature of 40 0 C is fed into a precision filter where it is further purified. Wood chips and / or sawdust can be used as a filtration element to more thoroughly clean the gas. After use in the filter, such a filter element can be added to the feed. The cleaned and purified gasification gas is sent to a chemical purification filter where it removes the residue of harmful gaseous components such as HCl, H ₂ S, SO ₂ etc.

[00159] The filter element of the filter is an iron oxide that purifies the gas passing through it: F
A porous solid structure composed of e ₂ O ₃ and FeO can be shown. Sulfur-containing and chlorine-containing components are bound on the surface of the filter element. The filter element is cleaned and regenerated by periodically passing a NaOH solution through it. The alkaline solution is a solution of sodium sulfide and chloride: Na ₂ S, NaCl, and some dissolved iron oxides as complex compounds of various compositions such as Na [Fe (OH) ₄ ], Na ₄ FeO ₃ etc. Including things.

[00160] Once the required concentrations of these materials in aqueous NaOH solution are achieved, replace the solution with a fresh one. The solution used, together with the particles of the filter element dissolved in it, such as Fe ₂ O ₃ and other compounds, is fed through the batch feeder into the feed for use as an additive. After the chemical purification filter, the gasification gas is sent into a gas holder where the composition is averaged. The gasified gas can then be used in gas-diesel, gas powered, or gas turbine aggregation devices for power generation.

[00161] hot flue gas having a temperature of about 900 ~ 950 ° C. to produce as a result of combustion of the gasification gas is fed into a second heat exchanger, is cooled here to approximately 200 ~ 250 ° C.. At the same time, water used for cooling is heated to about 60 ~ 80 ° C. in the first heat exchanger. Depending on the need and the structure of the second heat exchanger, process streams and hot water of various parameters can be obtained at the outlet for the heat exchanger. The water vapor portion can be sent to the gasifier as further oxidant through the separation channel.

[00162] Changes and modifications and alternatives to the above example can be derived from FIG. FIG.
Shows the technical scheme of the pressurized bed gasification process.
Example 2: Comparative characteristics of the main application technologies of solid household waste:
[00163] To confirm the efficiency of the pressurized bed gasification process with respect to the prior art, calculations were performed using a simplified approximate model. Thus, the results cannot be regarded as accurately reflecting the actual process. The main purpose of this calculation was to obtain data based on which a comparative analysis of the efficiency of technical schemes for the use of solid household waste can be performed.

[00164] The algorithm shown below is a series of steps to model the technology of bed gasification under pressure. The same principle can be used to account for differences between process technology schemes to calculate all other techniques. The initial conditions for all techniques are the same and are the composition of the feed, its drying and classification (for all techniques, loading with 10% moisture content and 10% inorganic component feed).

[00165] Feed material fed into the gasifier:
1.1. The calculation is based on the average morphological structure of solid household waste shown in the table below.

  1.2. Reference data on the elemental composition of each morphological group is estimated as follows.

  1.3. The elemental composition of the whole solid household waste is calculated based on the data on the morphological structure and the elemental composition of each form group. In the following calculations, the chlorine content in the feed is not taken into account for the sake of simplicity.

  1.4. After classification and drying, the feed composition is calculated. For all comparative calculations, the assumption was made that the residual minerals comprised 10% after classification and the moisture content was 10% after drying.

[00166] 2. Based on the calculated element of solid household waste, a composition factor for the charge feed formulation is determined.

[00167] 3. All further calculations are carried out per 1000 g of classified and dried feed, ie in this case per 1000 g of solid household waste having a moisture content of 10% and an inorganic content of 10%.

[00168] 4. Calculate the quantitative properties of the fuel based on the total formulation obtained-elemental weight in the fuel, molecular weight, amount of material, and heat of combustion.

[00169] 5. Calculation of calorific value of feed material 5.1. Calculation of combustion chamber composition without mineral content and moisture content:

  5.2. Based on the Mendeleev equation (339 C% + 1256 H% -109.8 (O% -S%) = Q) and the elemental composition, the calorific value of the fuel is calculated. Calculations are made at kJ / kg for the organic component of the fuel, classified fuel, and unclassified fuel, and kJ / mol for the classified fuel (the latter is for further calculation of the thermal effect of the reaction). Necessary for

5.3. Reference data of the base gases (CO, CH ₄ , H ₂ ) and carbon (C) heat of combustion are used for further calculation of the thermal effects.

[00170] 6. In the calculations, it is said that the processes of pyrolysis of the loaded feed and subsequent oxygen gasification (oxidation), hydrogasification of carbon formed during pyrolysis and carbon dioxide gasification occur continuously in the reactor Make assumptions.

[00171] 7. The thermal decomposition process is considered as a model reaction.
CHONS = C + CO + CH ₄ + H ₂ O + H ₂ S + N ₂ + H ₂
The coefficient for this equation can be varied depending on the composition of the feed used. The following assumptions are also used for the calculation of the pyrolysis process:

- In the pyrolysis stage, CO ₂ is either not formed or are completely consumed in other reactions.
-NO, NO _2, and other nitrogen oxides or not formed, or is consumed in other reactions.

  -Sulfur only forms hydrogen sulfide; however, under practical conditions, about 50% of the sulfur remains as sulfide in the residual slag and some of the sulfur can pass from the reactor as sulfur oxides There is sex.

7.2. The ratio of CO and H _{2 O} are formed can not be determined accurately based on the composition of the feed material. These data can only be obtained in a practical way. Thus, such a value is initially set in the calculation conditions as a percentage of oxygen changing from the feed to CO and H ₂ O.

7.3. Similarly, the ratio of CH ₄ and H ₂ cannot be set accurately. To determine such parameters, the percentage of hydrogen transferred from the initial feed material into products such as CH ₄ , H ₂ O, H ₂ S, and H ₂ is set.

  7.4. Based on the element weight in the feed and the set conditions for the distribution of hydrogen, carbon and oxygen, the coefficients in the pyrolysis equation are calculated.

  7.5. Based on the calculated reaction coefficients, a calculation is made of the weight and amount of gas and carbon obtained during the pyrolysis process.

[00172] 8. Oxidation with oxygen:
8.1. An amount of air is fed into the reactor. This calculation determines the amount of air that needs to be fed into the gasifier to remove the thermal energy in the combustion process of the portion of the feed material needed to maintain the gasifier heat balance .

  8.2. In order to simplify the calculation, we make the assumption that only carbon reacts with oxygen. In the actual process, first, the combustible gas formed during the pyrolysis process burns, and in parallel with this, the carbon portion burns. It is also assumed that the combustion process is complete and no product of incomplete combustion is formed.

C + O ₂ = CO ₂
8.3. In the calculation, excess added air may or may not be used.

  There is no excess air when reflected in the table below.

  8.4. First, an optional value of weight and amount of oxygen consumed according to which air nitrogen is added is introduced into the calculation.

8.5. The weight and amount of gasification products formed in the combustion of a portion of the feed (in this case carbon) and the weight of carbon consumed at this point are determined.
8.6. Based on the thermal effects of the carbon combustion reaction, the total amount of thermal energy generated in all necessary air oxygen interactions is determined.

[00173] 9. CO ₂ conversion-carbon dioxide gasification:
9.1. Some of the CO ₂ formed interacts with various solid or gas components. For the convenience of calculation, conversion of CO ₂ is considered to follow the following reaction.

CO ₂ + C = 2CO
The traditional parameter-CO ₂ conversion factor, which can be determined based on experimental data only, is introduced.

9.2. The conversion factor is used in the calculation to calculate the amount of CO ₂ and carbon to be reacted as well as the amount of CO formed.

[00174] 10. Hydrogen gasification:
10.1. Interaction of water vapor, the hypothetical is performed with the carbon remaining after the combustion and conversion CO _2.

_{C + H 2 O = CO +} 2H 2 O
This is the main reaction. In the actual reaction, many other products are formed after hydrogasification, but their amounts and effects are negligible.

  10.2. Consider the following types of water: The first is the moisture contained in the feedstock; the second is the added steam or water; the third is the water formed in the pyrolysis process. In some cases, the initial moisture content in the feed may be sufficient or exceed the required amount.

  In this case, the amount of water that needs to be added is calculated.

[00175] 11. Gas produced at the outlet of the gasifier:
11.1. The composition, weight, amount, heat content, and its methane equivalent of the gas produced at the outlet of the gasifier are calculated. The calculation is based on the composition of the generated pyrolysis gas. These data are summarized and the gasification gas at the outlet of the reactor is calculated.

[00176] 12. Energy loss:
In this case, the following energy loss: (1) endothermic reaction effect; (2) heat loss associated with slag removal; (3) loss due to gasifier design; (4) hot gas produced by the gasifier Consider losses associated with: (5) losses associated with water vapor formation from unreacted water.

12.1. Calculations of thermal reaction effects are partially performed using reference data of thermal reaction effects on the heat of combustion of individual substances.
Thermal energy of the thermal decomposition of the feed; (2) C + H ₂ O = CO + H ₂ ; (3) C + CO ₂ = 2 CO;

  12.2. Based on the calculated thermal reaction effect and the known amount of reactants, the amount of thermal energy absorbed or released during these reactions is calculated. The approximate (total) amount of thermal energy for all reactions is then calculated. In this case, a large amount of thermal energy absorption is observed.

12.3. Heat loss associated with slag removal:
Based on the heat capacity calculated, the average morphology of the slag, and its known amount and temperature, a calculation of heat loss associated with slag removal from the gasifier is made.

12.4. Loss related to gasifier design:
The heat loss through the gasifier vessel structure is determined by a number of factors and is very complicated for detailed and accurate calculations. In this case it is assumed that these losses constitute 5% of the total amount of energy introduced into the reactor.

12.5. Thermal energy extracted from the reactor with the gasification gas:
For each gas composition, heat capacity is calculated based on known reference factors. Using the calculated amount of gas and its temperature at the outlet from the gasifier, determine the amount of thermal energy extracted in their cooling to 25 ° C.

12.6. When excess moisture is introduced into the gasifier, it is also necessary to consider the energy consumption for the formation of water vapor from such moisture.
There is no excess of water in this example.

  12.7. Summarize the total heat loss of the gasifier.

[00177] 13. Energy loss compensation:
Compensate for thermal energy (see 8.6.) Released during carbon combustion. Thus, it is necessary to supply a predetermined amount of air (in which the amount of energy released corresponds to the amount of energy loss) into the reactor. First, assume an arbitrary amount of air supply (see 8.4.). After calculating the total energy loss, it is possible to determine that the energy released after combustion equals the total energy loss by means of a trial and error method which changes the amount of air supplied. The required amount of added air can then be calculated.

[00178] 14. After recovery, the gas is cooled to 40 ° C. and the heat transfer loss is 10% to calculate the amount of recovered thermal energy of the gasification gas.

[00179] 15. Generation of electrical energy:
Two options for electricity generation from gasification gas are considered in comparative calculations.
(1) Use of a gas driver having an efficiency factor of 38.7%;
(2) Use of a steam turbine with an efficiency factor of 20%.

  Depending on the parameters of the gas produced, it is possible to consider the possibility of producing electrical energy using a gas driver.

[00180] 16. Recovery of thermal energy of flue gas after gas drive:
In this calculation, from the total energy of the gasification gas,
38.7% is converted to electrical energy;
41.3% is converted to thermal energy which is recovered as outlet hot water or process stream;
20% is the loss associated with the reactor design and the loss associated with the emission of flue gas into the atmosphere (in this calculation, the temperature of the gas discharged from the heat exchanger is 250 ° C.);
Assume that

[00181] 17. Weight balance calculation:
The input weight is the sum of the weight of (a) the loaded material, (b) the supplied air, and (c) the additionally supplied water or steam. The output weight is composed of the weight of gasification gas generated and the weight of slag.

[00182] 18. Energy balance:
The energy input is the heat of combustion of the feed loaded into the gasifier. The energy produced is the sum of the heat of combustion of all the generated gasification gases and all the heat losses of the reactor (i.e. the heat of the gasification gases, the equipment losses, the heat energy taken with the slag, etc.).

  The table below illustrates some of the advantages of the present technology over previously known used techniques.

[00183] While the above disclosure illustrates the principles of the present invention by way of example given by way of illustration only, the use of the present invention is to be determined according to the claims appended hereto and all ordinary ones within the scope of equivalents thereof. It should be appreciated that it includes changes, adaptations, and / or modifications.

[00184] Those skilled in the art will recognize from the above that various adaptations and modifications of the just-described embodiment can be configured without departing from the scope and spirit of the present invention. It is therefore to be understood that within the scope of the appended claims, the invention may be practiced otherwise than as specifically described herein.

Claims (14)

Providing a gasifier trunk having a frusto-conical shape that widens towards the bottom;
Providing a loading mechanism trunk located at the top of the gasifier trunk;
Providing a combustion chamber at the bottom of the gasifier trunk and a slag discharge mechanism at the bottom of the combustion chamber;
It gives the following the (a) ~ (c) zone in this order to the gasifier trunk,
(D) to (f) zones are given in this order in the combustion chamber,
Provide (g) area within the slag discharge mechanism :
(A) drying area,
(B) plasticizing zone,
(C) low temperature pyrolysis zone,
(D) a high temperature pyrolysis zone,
(E) combustion area,
(F) a reforming zone; and
(G) Slag discharge area;
Supplying the feed material;
By a loading mechanism having a loading mechanism trunk and a feed supply device, the feed material is passed through the loading mechanism trunk and in the drying zone, plasticizing zone, low and high temperature pyrolysis zone, combustion zone, reforming zone, and slag discharge zone. Send through each;
Feed material sent through the loading mechanism trunk forms a plug in the loading mechanism trunk that hermetically separates the dry zone, plasticization zone, low and high temperature pyrolysis zone, combustion zone, reforming zone, and slag discharge zone from the atmosphere. And
Form and separate water vapor from the feed in the drying zone;
Forming pyrolysis gas in the pyrolysis zone;
Separating all of the pyrolysis gas from the feed in the pyrolysis zone, thereby separating the carbon char residue; and
Forming gasified gas in the combustion chamber ;
A downflow gasification method including a process. Forming a mixture with the separated pyrolysis gas and water vapor;
Moving the mixture to the combustion zone;
Burning the mixture in a combustion zone;
Burn a portion of the carbon char residue in the combustion zone; and use the remaining portion of the carbon char residue for the reforming reaction in the reforming zone;
The method of claim 1, further comprising a step.   The method of claim 2, further comprising supplying air to the combustion chamber.   The method according to claim 2, further comprising the step of supplying a mixture of oxygen and steam to the combustion zone.   The method according to claim 1, further comprising the step of converting hydrocarbons contained in the pyrolysis gas into hydrogen and carbon monoxide while being transferred through the combustion zone and the reforming zone.   The process according to claim 1, wherein the feed material comprises an inorganic component and is therefore subjected to purification as the gasification gas is moved through the combustion zone and the reforming zone.   The method according to claim 1, further comprising the step of adding at least one adsorbent to the feed. The method according to claim 7 , wherein the at least one adsorbent is a metal, an oxide, a salt or an oxide hydrate.   The method of claim 1, further comprising the step of adding at least one flux to the feed. 10. The method of claim 9 , wherein the at least one flux is a metal, an oxide, a salt, an oxide hydrate, a sulfide, or a chloride.   The method of claim 1, further comprising the step of adding silicon dioxide to the feed.   The method of claim 1, further comprising the step of providing steam into the combustion zone.   The method of claim 1, further comprising the step of supplying carbon dioxide into the combustion zone. Moving the gasification gas through at least one of a reforming zone, a combustion zone, a low temperature and high temperature pyrolysis zone, a plasticization zone, and a drying zone, thereby further reducing the temperature of the gasification gas The method of claim 1.

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